Phosphoric acid ammoniation process to produce liquid fertilizers
Phosphoric acid and ammonia are reacted together with additions of water when necessary in a reaction vessel to form a molten entrained stream reaction mixture to which a water quench is added to produce an ammonium polyphosphate liquid fertilizer.
This invention concerns the performance of fast and, usually, exothermic reactions between two or more reactants at least one of which is a liquid. The invention is more particularly applicable to reactions between acids, such as phosphoric acid, and bases such as ammonia and is especially applicable to the ammoniation of phosphoric acid and phosphoric acid containing polyphosphoric acid components.
Phosphoric acid and superphosphoric acid (the latter containing polyphosphoric acid components, that is, two or more orthophosphoric acid units condensed with the elimination of watermolecules) have been ammoniated in the past by feeding ammonia to an aqueous solution of the acid, accompanied by stirring and cooling to 180.degree. F. or lower temperatures in order to prevent hydrolysis of the polyphosphate components of the acid.
Phosphoric acid has also been ammoniated in a two stage process. In such a process, partial ammoniation is achieved in one reactor from which the intermediate product is pumped to a second stage reactor for completion of the ammoniation. Viscosity and the ability to pump the intermediate product is a function of pH and therefore the degree of ammoniation has to be carefully controlled in the first stage.
The above discussion indicates that there is a need for a process of ammoniating phosphoric acid in a single reactor and thereby eliminating the problems which are inherent in two stage ammoniation.
It is therefore an object of this invention to provide a novel process for accomplishing rapid reactions and, in particular, for accomplishing rapid ammoniation of phosphoric acid and other acids.
It is also an object of this invention to provide a process for the ammoniation of phosphoric acid which converts orthophosphoric acid to polyphosphoric acid and results in an ammoniated product containing polyphosphate values.
A further object is to provide apparatus for the performance of the process of the invention.
The invention will be explained in further detail with reference to the accompanying drawings, in which:
FIG. 1 is a schematic diagram;
FIG. 2 is a view partially in section of the reaction vessel of FIG. 1; and
FIG. 3 is a view, partially in section, of an alternate embodiment of the reaction vessel.
FIG. 4 is one embodiment of an apparatus that can be used in carrying out the process of this invention.
Like elements are identified by the same numerals in the different figures.
The invention will be described in relation to its application to the ammoniation of phosphoric acid which can contain polyphosphoric acid components. In this application, the process comprises mixing phosphoric acid, ammonia and water in a reaction zone. The ammoniation of phosphoric acid and/or superphosphoric acid proceeds rapidly with the evolution of heat. The amount of heat evolved is sufficient to convert the water that is present to steam and also to drive off some water of constitution from two or more molecules of orthophosphoric acid, pyrophosphoric, tripolyphosphoric acid and other polyphosphoric acids, ammonium orthophosphate, ammonium pyrophosphate, ammonium tripolyphosphate and ammoniated species of other polyphosphoric acids. The resulting product, in the presence of ammonia, is a mixture of ammonium phosphate and ammonium polyphosphates. If insufficient ammonia is present, the mixture then also contains orthophosphoric acid and polyphosphoric acid components. The term "poly-" as used in this writing includes species formed from the condensation of two or more orthophosphoric acid and/or orthophosphate molecules and therefore includes pyrophosphoric acid and ammonium pyrophosphate as well as tri-, tetra-, penta- and higher polyphosphoric acids and ammonium polyphosphates. As a result of the elimination of water of constitution at the high temperatures of 300.degree. F. to 700.degree. F. that are achieved in the reaction zone, at least a portion of the phosphate material in the feed components is converted to polyphosphates. In other words, in addition to ammoniating orthophosphoric and polyphosphoric acids, the present process provides a method for converting P.sub.2 O.sub.5 in the orthophosphate form to the polyphosphate form.
The water that is introduced into the reaction vessel is either present in the phosphoric acid solution that is used or is added as required in accordance with the teachings herein.
The steam that is formed in the reaction vessel builds up a pressure that aids in propelling the reaction mixture through and expelling it from the reaction zone. At elevated temperatures of from 400.degree. F. to 700.degree. F., the product is expelled in the molten state. Alternatively, the product can be quenched with water prior to or after discharge from the reaction vessel to form an aqueous ammonium phosphate and ammonium polyphosphate fertilizer solution. A 10-34-O (10% by weight nitrogen, 34% by weight P.sub.2 O.sub.5 and 0% K.sub.2 O) grade fertilizer is readily made by this process.
Steam separates from the product mixture upon discharge from the reaction vessel. In one of the embodiments of this invention a cooling tower is provided in which separation of product from steam is effected. This is more fully set forth below in the description relating to FIG. 4.
The reaction mixture remains in the reaction zone for a residence or retention time of from about 0.1 second to about 15 minutes. Retention times of shorter durations within such range are preferred. Good results are obtained, for example, when the retention time is from about 1 second to about 8 minutes. Especially preferred are the short retention times of from about 1 second to about 3 minutes. This is especially true at relatively high reaction temperatures.
The reaction mixture in the reaction zone is maintained at a temperature within the range of from about 150.degree. F. to about 700.degree. F. At lower temperatures the reaction period (or retention time) can be for a much longer duration than at higher temperatures. This is the reason for the spread in the length of retention times which were discussed above. Although reaction temperatures in the range of 150.degree. F. to 700.degree. F. can be employed, it is preferable to employ temperatures of from about 225.degree. F. to about 600.degree. F. which provide for a readily controllable reaction rate. Especially preferred is a reaction temperature range of from about 450.degree. F. to about 575.degree. F. The product is discharged from the reaction vessel either as a melt at approximately the reaction vessel temperature or it is quenched with water and discharged at temperatures in the range of 100.degree. F. to 250.degree. F. Preferably the product is discharged at a temperature in the range of 150.degree. F. to 225.degree. F. and then promptly cooled to 150.degree. F. and lower.
An alternate embodiment of this invention is to employ in the reaction mixture only a part of the ammonia required to form an end product having a predetermined pH of from about 3.5 to about 0.5 Additional ammonia can then be added to the cooler reaction product after it has been discharged from the reaction vessel in an amount sufficient to produce an end product having the desired composition and pH.
An alternate embodiment of this invention is to employ in the reaction mixture only a part of the water required to form an end product having a predetermined specific gravity. After the reaction product mixture has been discharged from the reaction vessel, water is added in an amount sufficient to obtain an end product of the desired composition and having a predetermined specific gravity.
The end product can be further cooled to about 60.degree. F. to 120.degree. F. by passing it in heat exchanging relationship with ammonia or by other conventional cooling means. Preferably, the ammonia employed for this purpose is the ammonia which is used in carrying out the process of this invention. In this case at least a portion of the liquid ammonia is gasified by this means.
In one embodiment of this invention there is included the step of measuring the specific gravity of the end product and adjusting the amount of water employed in the method to provide an end product which has a predetermined specific gravity. The specific gravity is a function of the end product with regard to specific nitrogen and phosphorus analysis. For example, the specific gravity of the product 11-37-0 is in the range of 1.25-1.45. The specific gravity of 10-34-0 is in the range of 1.34-1.43. The specific gravity of 12-43-0 is in the range of 1.42-1.55. The specific gravity of 8-24-0 is about 1.28. Generally the specific gravity can vary from about 1.25 to about 1.55.
An embodiment that can be used in this invention is to conduct the ammoniation under a pressure of from about 0.1 to about 100 psi (pounds per square inch as measured by a gauge) in the reaction vessel. A preferred range of pressures when ammoniating phosphoric acid having a P.sub.2 O.sub.5 content of from about 30% to about 68% is 10-60 psi. An especially preferred range for conversion of the phosphates to polyphosphates is 20 to 40 psi. When pressures are employed, suitable pumps are employed in the acid, water and ammonia feed lines to facilitate introduction of the reactants into the reaction vessel.
Another embodiment that can be used in this invention is to preheat the feed acid. This permits the achievement of a higher temperature in the reaction vessel in a shorter period of time which, in turn, permits the use of a shorter retention time. Preheating can be accomplished by any conventional means. A preheating of the feed acid having a 30%-68% P.sub.2 O.sub.5 content to a temperature of from 70.degree. F. to 575.degree. F. results in a higher percentage conversion of the phosphates to polyphosphate components in the reactor. A preferred range of preheating temperatures is 150.degree. F. to 450.degree. F. When the acid is preheated to its boiling point, a concentration to a higher P.sub.2 O.sub.5 content is achieved. For example, a 30% P.sub.2 O.sub.5 acid heated to 500.degree. F. is concentrated to approximately 65% P.sub.2 O.sub.5. Such concentration during preheating is sometimes referred to as preconcentration.
A further embodiment that can be employed is to preheat, by any conventional means, in addition to those shown in the drawings, the water and ammonia that is admitted to the reaction vessel. The water can be preheated to a temperature within the range of 70.degree. F. to 99.degree. F. Water that is heated to a temperature of from 85.degree. F. to 95.degree. F. gives good results and preheating to within this range constitutes a preferred embodiment of this invention. The anhydrous ammonnia can be vaporized and introduced into the reaction vessel at temperatures ranging from just above the boiling point of ammonia to about 500.degree. F., that is, a temperature within the range of -27.degree. F. to 500.degree. F. It is preferred, however, to preheat the ammonia to a temperature of from 50.degree. F. to 200.degree. F. Temperatures within this range are readily attainable by the process of heat exchanging either with the product which is discharged from the reaction vessel or by other conventional means. A heating coil in an external heater (not shown) is used when the ammonia is preheated to a temperature of 80.degree. F. or higher.
In FIG. 1, either wet process or furnace phosphoric acid, anhydrous ammonia and water, one or all of which can be preheated as previously described, are admitted into reaction vessel 1 through conduits 2, 3 and 4, respectively. When the phosphoric acid is preheated, it is introduced through conduit 101, valve means 102, heat exchange means 103, and conduit 2 to the reaction vessel 1. Heat can be supplied to the heat exchange means 103 in any conventional manner. Wet process acids contain small amounts of iron and aluminum impurities as well as impurities of other substances found in phosphate bearing ores. The phosphoric acid, water and ammonia are metered into the reaction vessel by conventional metering apparatus such as a metering pump or magnetic flow meter (not shown). Ammonia reacts with the acid to form ammonium phosphate and ammonium polyphosphate with the liberation of heat. The amount of water added to the reaction vessel together with the phosphoric acid and ammonia is sufficient to keep the temperature of the reaction mixture within the range of 150.degree. F. to 700.degree. F. Additional water is added as necessary to quench the reaction product.
The heat liberated upon ammoniation of the acid is sufficient to convert part of the water to steam as the reaction mixture progresses through the reaction vessel. By suitable adjustment of valve means 6 and 8, additional water can be admitted through conduit 5, valve means 6 and conduit 7 into the reaction vessel near the product exit port. The water quenches the reaction mixture so that it can be discharged from the reaction vessel into the receiving vessel 9 at a temperature of 100.degree. F. to 250.degree. F. Preferably, it is discharged at a temperature of 180.degree. F. or lower, or quickly cooled in the receiving vessel by suitable means (not shown) to 180.degree. F. or lower in order to minimize hydrolysis of the polyphosphates.
The reaction product mixture can be transferred through conduits 10 and 11 to storage either by gravity or with the aid of pump 12. Should it be desirable to lower the temperature of the reaction product or to preheat the ammonia, it may be passed in heat exchanging relationship with ammonia through the heat exchanging means 13 and then conducted to storage.
Ammonia is fed in through inlet 14, heat exchanger 13, conduit 15, valve 16, meter 17, and conduit 3 to the inlet to reaction vessel 1.
Water employed in the process is fed to the inlet of conduit 30 through conduit 31, valve 32, meter 33 and conduit 4 to the water inlet to reaction vessel 1. The water can be preheated in heat exchange means 41 by the product passing through conduits 18, 40, 104, valve means 105 and conduit 106 to storage. The heat exchange means 41 can, of course, be mounted in conduit means 11. Should it be so desired, a portion of the product can be recycled through conduit 42 and valve means 43 to the receiving vessel 9.
The ammonia and phosphoric acid can be admitted to the reaction vessel in the correct proportions to obtain a reaction product having the desired pH. Alternatively, a portion of the reaction product is routed through conduits 19, 119, pH meter-controller 20 and conduit 21, back to the receiving vessel 9. The pH meter-controller monitors the pH of the reaction product and provides an electrical outlet signal of a phase and magnitude proportional to the direction and degree of deviation of the measured pH from a predetermined pH set in the instrument. Equipment for measuring the pH and providing a pH meter-controller output signal is readily available commercially and will not be further described here. A valve 99 in ammonia conduit 15 is actuated by valve actuator 22 in response to the output signal from the pH meter-controller 20 received through electrical conductor 23. Valve actuator 22 controls the opening in valve 99 to increase or decrease the flow of ammonia therethrough so as to bring the pH of the reaction product back to the predetermined pH set on the pH meter-controller instrument. For example, when the pH is higher than the predetermined value, the opening in valve 99 is reduced thereby reducing the flow of ammonia therethrough, which will have the effect of producing a reaction product with a lower pH. On the other hand, if the pH is too low, valve actuator 22, in response to the signal from the pH meter-controller, turns valve 99 to increase the opening therethrough, allowing ammonia to flow through conduit 15 at a higher rate to thereby provide a product with a higher pH.
An alternate embodiment of this invention is to take from about 1% to about 30% of the ammonia employed in the process and feed it directly to the reaction product mixture in receiving vessel 9 through conduit 24, valve 25, meter 26 and conduit 27. Valves 16 and 25 can be adjusted, for example, to permit about 85% of the ammonia used in the process to flow through conduit 3 to the inlet to reaction vessel 1 and about 15% to flow through meter 26 and conduit 27 to the reaction product receiving vessel where the reaction product mixture is further ammoniated. The ammonia can be bubbled into the reaction product mixture through a sparger, not shown, located near the bottom of the vessel. The total amount of ammonia employed in the process is controlled by the pH meter-controller 20.
A specific gravity indicator-controller 28 can be mounted in conduit means 19-119 to monitor the specific gravity of the portion of reaction product that is being circulated through conduits 19, 119, pH meter-controller 20 and back to the receiving vessel 9 through conduit 21. The specific gravity indicator-controller monitors the specific gravity of the reaction product mixture and provides an electrical output signal through electrical conductor 29 of a phase and magnitude proportional to the direction and degree of deviation of the specific gravity from the predetermined specific gravity which has been set on the specific gravity indicator instrument. Equipment for measuring specific gravity and providing a specific gravity controller output signal is readily available commercially and will not be described here.
Valve 34 in conduit 31 is controlled by valve actuator 35 and controls the amount of water flowing through conduit 31. Valve controller 35 is responsive to the output signal from specific gravity indicator-controller 28 and increases or decreases the opening in valve 34 so as to permit that amount of water to flow therethrough which will provide an end product having predetermined specific gravity. For example, if the specific gravity is too low the valve controller 35 will decrease the opening in valve 34 to permit less water to flow therethrough, thereby increasing the density of the reaction product. On the other hand, if the specific gravity of the reaction product is too high, the valve controller 35, in response to the signal from the specific gravity indicator-controller 28, will operate valve 34 to increase the opening therethrough, allowing more water to flow through conduit 31, thereby providing a product having a lower specific gravity.
An alternate embodiment of this invention is to take from about 1% to about 30% of the water flowing through control valve 34 and route it through conduit 36, valve 37, meter 38 and conduit 39 to the receiving vessel 9. For example, the total amount of water employed in the process can be divided to provide for a flow of about 80% of such water through meter 33 to the reaction vessel 1 and 20% of the water through meter 38 and conduit 39 to the reaction product receiving vessel 9.
The reaction vessel means 1, shown in FIG. 2, has a fluid receiving means 51 with one end thereof extending into the interior of column means 72. The fluid receiving means 51 is equipped with inlet means 52, 53 and 54 for acid, ammonia and water, respectively. The fluid receiving means can also be equipped with means for attaching pressure indicating devices and other instruments as at 55. The end 56 of the fluid receiving means 51, which is encompassed by the closed end 57 of the column 72, has a closed end 58 and a plurality of apertures 59 in the walls communicating between the interior of the fluid receiving means 51 and the interior of the column 72. The number and size of the apertures in the end 56 depend on the capacity of the apparatus, that is, the volume of reaction mixture components required to pass therethrough per unit time. The apertures can be circular, square or any other desired shape. It is found that circular apertures having a diameter of from about 1/16 inch to about 3/4 inch, or higher, are satisfactory for the process of this invention. Circular apertures having a diameter of from about 1/8 to about 3/8 inch are preferred since they impart a good degree of mixing to the components as they pass therethrough. Especially preferred are circular apertures having a diameter of 1/4 inch as these provide for good mixing of product. The apertures can be spaced from about 1/4 inch apart, in the case of apertures having a diameter of 1/8 inch, to about 11/2 inches apart in the case of apertures having a diameter of 3/4 inch. Apertures having a diameter of 1/4 inch can be spaced from about 3/8 to about 3/4 inch apart. Apertures having a diameter of 1/4 inch disposed about 1/2 inch apart in the walls of the end 56 of the fluid receiving means 51 are found to perform satisfactorily for the process of this invention.
The apertures 59 in end 56 of the fluid receiving means 51, in diameter and number should be such as to provide a pressure drop for fluid passing therethrough in the range of about 0.1 to about 100 psi. It is preferred that the pressure drop be within the range 10 to about 60 psi for thorough mixing of the components of the reaction mixture passing therethrough. In order to maintain a predetermined pressure within the reaction vessel, the outlet 112 of the reaction vessel can be closed off and equipped with a valve means, not shown.
The column 72 is composed of a plurality of cylindrical sections 60. A flange or other means at each end of a section permits the sections to be stacked and fastened together by means of bolts or other retaining means as shown in the drawing. The section 57 which encompasses end 56 of the fluid receiving means 51 also has a flange or other means at the open end thereof adapted for mounting said fluid receiving means 51 on to one end of the column 72. A plurality of plate members 61 having a plurality of apertures in each, obturate the column in spaced apart relationship. A plate member 61 is mounted in between two section of the column at a plurality of junctions of such plurality of sections 60. The apertures 62 in plates 61 can have the same characteristic as the apertures in the walls 56 of the fluid receiving means 51. When the apertures are circular, the diameter thereof can vary from about 1/16 inch to about 1 inch. Apertures having a diameter of from about 1/4 to about 3/4 inch are found to serve satisfactorily in providing a means for mixing the components making up the reaction mixture in this invention. A water inlet means 111 is provided near the bottom of the column 72 through which water is introduced for quenching or cooling, or for adjustment of the product composition of the reaction product mixture.
Suitable packing 63 is disposed in the column 72 between the plate members 61. The requirement of the packing is that it provides for a mixing of the components passing therethrough in order to enhance the efficiency of ammoniation of the acid. Suitable packing material for example is 1/8 to 2 inch stainless steel pipe cut into sections of 1/4 inch to about 2 inches. Pall or Raschig packing, berl saddles, grid packing and spiral grids are examples of other packing material that can be employed. The material of construction of the equipment used in the process of this invention can be any corrosion resistant material such as, for example, stainless steel.
FIG. 3 shows an alternate embodiment of a reaction vessel comprising fluid reactor means and columnar vessel means, that can be used in carrying out the process of this invention. The reaction vessel 200 has an inner hollow element 201 which can be elongated or tubular in design, and an outer jacket means 202 providing an annular passageway 206 therebetween. The element 201 has an inlet end 211 (which is also the inlet to vessel 200) and a terminal end 212 made up of a plurality of hollow sections 203 connected end-to-end. The walls of each of the sections are perforated with a plurality of holes 208 to permit fluid to pass in and out of the coaxial passageway within the elements 203. A plurality of partition means or plate members 204 obturate the passageway in spaced apart relationship. A partition means is positioned between two successive sections 203 at a plurality of junctions of such sections and is held in place by a coupling member 205 which is used to fixedly join together two ends of two sections 203. The annular passageway 206 is obturated by a plurality of annular baffle members 207 between the inner wall of jacket means 202 and the outer walls of the element 201. An individual such annular baffle member 207 is located intermediate each pair of successive plate members 204. A tortuous path is thus provided whereby the reaction mixture is required to pass through the holes 208 from the inside of one member 203 into the annular passageway 206 and back into the inner passageway of an adjoining section 203. Good mixing of the compounds of the reaction mixture is thus accomplished.
The end of the outer jacket means 202 near the inlet end 211 of the vessel 200 contacts the element 201, as by a reducing member 209 or other means, to form an upper closure to the annular passageway 206. Inlet element 210 is connected to the inlet end 211 of the inner element 201 and has inlet means 213, 214 and 215 through which are introduced phosphoric acid, ammonia and water into the reaction vessel. The outer jacket member 202 terminates in an outlet end 216. The terminal end 212 of the element 201 can be disposed within the outer jacket means 202, near the outlet end 216 thereof. Alternatively, the terminal end 212 can be extended with a portion of a perforated section 203 and connected to the outlet end 216. If desired, in order to maintain a predetermined pressure within the reaction vessel, the outlet 216 of the reaction vessel 200 can be equipped with a valve means, not shown. The reaction vessel 200 can also be equipped with means for attaching temperature or pressure indicating devices or other instruments as at 218. Inlet means 217 are provided in the outer jacket means 202 adjacent the ends 212 and 216. Water and/or other materials can be introduced through such inlet means. In the manufacture of ammonium phosphate and/or polyphosphate fertilizers, water is added either through inlet element 210 or 217, or both, to provide a fertilizer composition.
The number and size of the holes 208 in the element 201 depend on the desired capacity of the apparatus, that is, the volume of reaction mixture components required to pass therethrough per unit time. The holes can be circular, square or any other desired shape. It is found that circular holes having a diameter of from about 1/16 inch to about 3/4 inch, or higher, are satisfactory for the process of this invention. Circular holes having a diameter of from about 1/8 inch to about 3/8 inch are preferred in element 201 since a good degree of mixing of the components is achieved with such an element. Especially preferred is an element 201 having circular holes with a diameter of 1/4 inch, as good mixing of product is then accomplished. The holes can be spaced from about 1/4 inch apart in the case of holes having a diameter of 1/8 inch, to 11/2 inches apart in the case of holes having a diameter of 3/4 inch. Holes having a diameter of 1/4 inch can be spaced from about 3/8 to about 3/4 inch apart. Element 201 with holes having a diameter of 1/4 inch disposed about 1/2 inch apart in the walls thereof are found to perform satisfactorily for the process of this invention.
FIG. 4 shows the relationship between the reaction vessel enclosed by columnar vessel means means 1, the cooling column means 306 and the receiving vessel means 9 which constitutes one of the embodiments of this invention. The reaction vessel means 1 is connected via connecting means 81 (which is one end of a columnar vessel means, the other end of which encloses the reaction vessel, as shown in FIG. 2) to a distributor means 82 which extends into the interior of the upper end of the cooling column means 6. The distributor means 82 is closed at its free end 83 and has a plurality of apertures 84 in the walls thereof communicating between the interior of the distributor means and the interior of the cooling column means. The apertures 84 can have the same characteristics as the apertures in the walls 56 of the fluid receiving means 51. When the apertures 84 are circular, they have a diameter within the range from about 1/16 inch to about 3 inches. Preferably, the diameters range from about 1/8 inch to about 2 inches as apertures of this diameter function satisfactorily in the process of this invention.
The cooling column means has a vent means 85 at its upper end to vent steam, water vapor and air. The lower end of the cooling column means has a reaction product outlet means 88 communicating with inlet means 98 to a reaction product receiving vessel means 9.
A de-entrainment means 86 is interposed between the distributor means 82 and the vent means 85 to prevent any reaction product mixture from being carried out of the vent means. An air supply means 307, such as a blower fan, for example, is connected to inlet means 87 near the bottom of column means 6. Air is supplied in this manner for counter current heat exchange and evaporative cooling with the downward flowing reaction product mixture coming from the reaction vessel means 1 and flowing into the cooling column through apertures 84 in the distributor means 82. Suitable packing material (not shown) is disposed in the cooling column between the distributor means 82 and the outlet means 88. The packing material can be made up of sections of stainless steel pipe of from about 1/4 inch to about 2 inches in length and from about 1/4 inch to about 3 inches in diameter, grid packing or of other suitable packing material. The packing material is retained within the column by a suitable retaining means (not shown) such as a perforated plate or grate means or the like.
The reaction product receiving vessel 9 rests on support means 89. The bottom of the reaction product receiving vessel is indicated in dotted outline 90, showing outlet means 91 communicating with outlet conduit 92.
The reaction vessel 9 rests on support means 89. The bottom of the reaction product receiving vessel is indicated in dotted outline 90, showing outlet means 91 communicating with outlet conduit 92.
The de-entrainment means 86 consists of material such as stainless steel wool, knitted polypropylene, teflon or glass. Alternatively, the de-entrainment device can consist of a tower in which gases ascend through a spiral path causing the entrained reaction product mixture liquid to separate out and return downwardly to the cooling column. Still other forms of de-entrainers are well known to those skilled in the art.
It has been found that when a liquid fertilizer product is made by the process of this invention, it is a stable liquid having a pH of from about 3.5 to about 8.5 and at the highest pH levels is non-corrosive to mild steel. Although the product contains impurities in the cases where the phosphoric acid was derived from wet-process phosphoric acid, the impurities do not precipitate out on long standing at temperatures of from about 0.degree. F. to about 120.degree. F.
The advantages obtained by use of the process of this invention include lower initial capital outlay, lower operating costs, high polyphosphate yields, control simplicity, reduced space requirements and lower maintenance costs.
The process of this invention is illustrated by the non-limiting examples given below. In these examples, preheating of the phosphoric acid to boiling can produce concentration, or preconcentration as it is sometimes called, to higher P.sub.2 O.sub.5 content. For example, wet process phosphoric acid containing impurities as set forth in the examples and having a P.sub.2 O.sub.5 content of 54%, will boil at about 280.degree. F. Therefore, a 30% P.sub.2 O.sub.5 acid preheated to boiling at 280.degree. F. is preconcentrated to 54% P.sub.2 O.sub.5. In like manner, a wet process acid heated to boiling at 400.degree. F. is preconcentrated to about 63% P.sub.2 O.sub.5 under a pressure of about 25 psi and to about 50% P.sub.2 O.sub.5 under pressure of about 100 psi. At 500.degree. F. the preconcentration under similar pressures ranges from about 66.5% P.sub.2 O.sub.5 to about 53% P.sub.2 O.sub.5. At 575.degree. F. the preconcentration would be from about 67% to about 54% P.sub.2 O.sub.5 under pressures of from about 25 psi to about 100 psi. The amount of preconcentration for any temperature and pressure is readily determined and ascertained by those skilled in the art. Such preconcentration, when desired, is an added benefit of the process of this invention. However, it is preferred to pressurize the feed acid sufficiently to prevent boiling at the temperature to which the acid is heated, prior to its introduction into the reaction vessel, in order to prevent deposition of scale impurities. In the absence of boiling, there is no concentration or preconcentration. Concentration occurs in the reaction vessel where boiling takes place at lower pressures and/or high temperatures. In the examples, the phosphoric acid added to the reaction vessel includes the water content corresponding to the concentration stated prior to preheating.
EXAMPLE ITo a reaction vessel of the kind shown in FIG. 3 is added wet process phosphoric acid solution with an analyses showing in percent by weight 52.55% P.sub.2 O.sub.5, 0.94% Fe.sub.2 O.sub.3, 2.25% Al.sub.2 O.sub.3, 0.45% MgO, 4.56% SO.sub.4, 2.54% water insoluble solid, and the balance being substantially water. The phosphoric acid is added at the rate of about 767 parts by weight per hour at a temperature of 250.degree. F. Water at 90.degree. F. is added through inlet 215 at a rate of about 50 parts by weight per hour. Anhydrous ammonia at a temperature of 100.degree. F. is added at a rate of about 125 parts by weight per hour. The temperature and pressure in the reaction vessel are maintained at about 450.degree. F. and 20 psi. respectively. The retention time in the reaction vessel is about 20 seconds. The fertilizer product is discharged from the vessel at a temperature of about 490.degree. F. Analyses show that the product contains, in percent by weight 43% P.sub.2 O.sub.5, 12% N (Nitrogen) and 0.91% solids. The amount of P.sub.2 O.sub.5 converted from the phosphate form to the polyphosphate form (conversion) is 38.5%. The melt product has a pH of 6.65 and a N/P.sub.2 O.sub.5 ratio of 0.286 and is classified as an ammonium polyphosphate solid when cooled.
EXAMPLE IIThe procedure of example I is followed with the modification that water is added through inlet means 217 at a rate of about 500 parts by weight per hour, phosphoric acid is added at a rate of 635 parts by weight per hour, and anhydrous ammonia at a temperature of 100.degree. F. is added at a rate of about 125 parts by weight per hour. The temperature and pressure in the reaction vessel are maintained at 450.degree. F. and 20 psi respectively. The retention time in the reaction vessel is about 20 seconds. The liquid fertilizer produced is discharged from the vessel at a temperature of about 165.degree. F. and cooled to 100.degree. F. Analyses shows the product contains, in percent by weight, 32.04% P.sub.2 O.sub.5, 12% N (nitrogen) and 0.91% solids. The amount of P.sub.2 O.sub.5 converted from the orthophosphate form to the polyphosphate form (conversion) is 37.55%. The liquid fertilizer produced has a pH of 5.70, a specific gravity (Sp. Gr.) of 1.393 and a N/P.sub.2 O.sub.5 ratio of 0.304 and is classified as a 10-34-0 liquid fertilizer.
EXAMPLE IIIThe procedure of Example II is repeated with the water being added through inlet means 215 at start up and after two minutes is all added through inlet means 217 near the product discharge port where it serves to quench the molten product mixture. A product of the kind described in Example II is obtained.
EXAMPLE IVTo a reaction vessel of the kind shown in FIG. 3 is added wet process phosphoric acid solution with an analyses showing in percent by weight 54% P.sub.2 O.sub.5, 1.1% Fe.sub.2 O.sub.3, 1.9% Al.sub.2 O.sub.3, 3.1% SO.sub.3 and 0.1% water insoluble solids. The phosphoric acid under a pressure of 150 psi is added at the rate of 920 parts by weight per hour at a temperature of 500.degree. F. without preconcentration. Water at 99.degree. F. is added through inlet 217 at a rate of about 1100 parts by weight per hour. Anhydrous ammonia at a temperature of 250.degree. F. is added at a rate of about 200 parts by weight per hour. The temperature and pressure in the reaction vessel are maintained at about 640.degree. F. and 100 psi respectively. The retention time in the reaction vessel is about 7 minutes. The liquid fertilizer product is discharged from the vessel at a temperature of about 250.degree. F. Analyses show that the product contained, in percent by weight, 24.5 P.sub.2 O.sub.5, 8.4% N and 0.2% solids. The amount of P.sub.2 O.sub.5 converted from the phosphate form to the polyphosphate form (conversion) is 65%. The liquid fertilizer product has a pH of 7.5, a specific gravity of 1.300 and a N/P.sub.2 O.sub.5 ratio of 0.344 and is classified as a 8-24-0 liquid fertilizer.
The procedure of Example IV is repeated with a retention time of 15 minutes. A good 8-24-0 liquid fertilizer product is obtained.
The procedure of Example IV is repeated with the modification that the phosphoric acid contains 30% P.sub.2 O.sub.5 and is heated to 450.degree. F. under a pressure of 75 psi and is added to the reaction vessel at the rate of 920 parts by weight per hour. Water is admitted to the reaction vessel at the rate of 650 parts by weight per hour and ammonia at the rate of 125 parts by weight per hour. The temperature and pressure in the reaction vessel are maintained at 600.degree. F. and 10 psi respectively. A good product is obtained.
The procedure of Example IV is repeated with the modification that the phosphoric acid is preconcentrated at 500.degree. F. and a pressure of 50 psi prior to admission to the reaction vessel which was maintained at a pressure of 60 psi. A good product is obtained but some scale deposition is noted in the apparatus.
The processes of Examples I through IV are also followed with the variation that the amounts of ammonia and water employed are controlled by the pH meter-controller and specific gravity controller as shown in FIG. 1 and as described elsewhere in this specification. Equally good results are obtained.
EXAMPLE VTo a reaction vessel of the kind shown in FIG. 3 is added wet process phosphoric acid solution with an analyses showing in percent by weight 54.4% P.sub.2 O.sub.5, 1.6% Fe.sub.2 O.sub.3, 1.1% Al.sub.2 O.sub.3, 2.2% SO.sub.3 and 0.7% water insoluble solids. The phosphoric acid, at a temperature of 300.degree. F. and 100 psi pressure is added without preconcentration at the rate of about 800 parts by weight per hour. Water at 95.degree. F. is added through inlet 217 at the rate of about 600 parts by weight per hour. Anhydrous ammonia at a temperature of 200.degree. F. is added at a rate of about 280 parts by weight per hour. The temperature and pressure in the reaction vessel are maintained at about 450.degree. F. and 25 psi respectively. The retention time in the reaction vessel is about 8 minutes. The liquid fertilizer product is discharged from the vessel at a temperature of about 150.degree. F. Analyses show that the product contains, in percent by weight, 33.38% P.sub.2 O.sub.5, 10.17% N and 0.1% solids. The amount of P.sub.2 O.sub.5 converted from the phosphate form to the polyphosphate form (conversion) is 32%. The liquid fertilizer product has a pH of 5.95, a specific gravity of 1.398 and a N/P.sub.2 O.sub.5 ratio of 0.305 and is classified as a liquid fertilizer.
The procedure of Example V is repeated with a reaction temperature of 300.degree. F., a retention time of 3 minutes and a reaction vessel pressure of 20 psi. A product of the kind described in Example V is obtained.
The procedure of Example V is repeated with the modification that the phosphoric acid is preheated to a temperature of 450.degree. F. and the water input is increased to 660 parts by weight per hour. The reaction vessel temperature is maintained at about 600.degree. F. The conversion to polyphosphate is about 75%.
EXAMPLE VITo a reaction vessel of the kind shown in FIG. 3 is added wet process phosphoric acid solution with an analyses showing in percent by weight 60.4% P.sub.2 O.sub.5, 2.2% Fe.sub.2 O.sub.3, 3.8% Al.sub.2 O.sub.3, 5.5% SO.sub.3 and 2.8% water insoluble solids. The phosphoric acid under a pressure of 100 psi is added without boiling at the rate of about 1100 parts by weight per hour at a temperature of about 575.degree. F. Water at 85.degree. F. is added through inlet 217 at a rate of about 550 parts by weight per hour. Anhydrous ammonia at a temperature of 50.degree. F. is added at a rate of about 254 parts by weight per hour. The temperature and pressure in the reaction vessel are maintained at about 575.degree. F. and 40 psi respectively. The retention time in the reaction vessel is about 1 second. The liquid fertilizer product is discharged from the vessel at a temperature of about 100.degree. F. Analyses show that the product contains in percent by weight, 32.65% P.sub.2 O.sub.5, 10.17% N and 0.13% solids. The amount of P.sub.2 O.sub.5 converted from the phosphate form to the polyphosphate form (conversion) is 75%. The liquid fertilizer product has a pH of 6.2, a specific gravity of 1.393 and a N/P.sub.2 O.sub.5 ratio of 0.314 and is classified as a 10-34-0 liquid fertilizer.
EXAMPLE VIITo a reaction vessel of the kind shown in FIG. 3 is added wet process phosphoric acid solution with an analyses showing in percent by weight 68% P.sub.2 O.sub.5, 2.1% Fe.sub.2 O.sub.3, 2.3% Al.sub.2 O.sub.3, 2.7% SO.sub.3 and 5.2% water insoluble solids. The phosphoric acid, at a temperature of 70.degree. F. is added at the rate of about 2,000 parts by weight per hour. Water at 70.degree. F. is added through inlet 217 at a rate of about 1,000 parts by weight per hour. Anhydrous ammonia at a temperature of -27.degree. F. is added at a rate of about 505 parts by weight per hour. The temperature and pressure in the reaction vessel are maintained at about 650.degree. F. and 10 psi respectively. The retention time in the reaction vessel is about 0.1 second. The liquid fertilizer product is discharged from the vessel at a temperature of about 225.degree. F. Analyses show that the product contains, in percent by weight, 32.74% P.sub.2 O.sub.5, 9.42% N and 1.00% solids. The amount of P.sub.2 O.sub.5 converted from the phosphate form to the polyphosphate form (conversion) is 85%. The liquid fertilizer product has a pH of 5.6, a specific gravity of 1.387 and a N/P.sub.2 O.sub.5 ratio of 0.290 and is classified as a 10-34-0 liquid fertilizer.
The procedure of Example VII is repeated with the phosphoric acid being added at a temperature of 150.degree. F. The process is carried out at a reaction temperature of 700.degree. F. and a reaction pressure of 0.1 psi. A product of the kind described in Example VII is obtained.
EXAMPLE VIIITo a reaction vessel of the kind shown in FIGS. 1, 2 and 4 were added superphosphoric acid having a P.sub.2 O.sub.5 content of 72 wt. %, at the rate of about 88 parts by weight per hour; anhydrous ammonia, 21 parts by weight per hour, and water, 110 parts by weight per hour. The pressure drop across the reaction vessel was about 40 psi. The reaction product mixture was discharged from the reaction vessel after a retention time of about 0.1 second, at a temperature of about 230.degree. F., into a cooling vessel comprised of a cooling column where it was cooled by a counter current air stream flowing at the rate of about 100 scfm per ton of reaction product mixture throughput per hour. The air and steam were vented as described above. The reaction product mixture was cooled to about 110.degree. F. at which temperature it was discharged into a receiving vessel. To the receiving vessel were added 2.5 parts by weight of anhydrous ammonia and 11 parts by weight of water, per hour. The amounts of ammonia and water used with the phosphoric acid was controlled by the pH meter-controller and the specific gravity indicator controller, respectively, as described above. The 10-34-0 product formed had a pH of 6.8, a specific gravity of 1.40 and 57.1% of the P.sub.2 O.sub.5 was in poly form. The product was further cooled to about 100.degree. F. and conducted from the receiving vessel to storage.
Good results are also obtained when the procedure of Example VIII is followed with the modification that the counter current cooling air stream flows at a rate of about 50 scfm per ton of reaction product throughput per hour.
The procedure of Example VIII is followed with the modification that additional water is used to make an 8-24-0 product having a specific gravity of 1.28. The product is discharged from the reaction vessel at 225.degree. F. and then cooled to 120.degree. F.
EXAMPLE IXThe procedure of Example VIII is followed with modifications in which the retention time is permitted to vary from 0.1 seconds to 8 minutes. A good 10-34-0 product is obtained at such retention times.
EXAMPLE XThe procedure of Example VIII is followed with the modification that the reaction product is cooled by the addition of the 11 parts by weight of water through inlet 111 to the reaction vessel 1 shown in FIG. 2. The reaction mixture is discharged from the reaction vessel 1 into the receiving vessel 9, without using the cooling vessel 6. The 2.5 parts by weight of anhydrous ammonia are added to the receiving vessel per hour and product of the kind described in Example VIII is obtained.
EXAMPLE XITo a reaction vessel of the kind used in Example VIII were added superphosphoric acid having a P.sub.2 O.sub.5 content of 73.1 wt. %, at the rate of about 30.9 parts by weight per hour; anhydrous ammonia, 7.5 parts by weight per hour; and water, 35 parts by weight per hour. The pressure drop across the reaction vessel was about 28 psi. The reaction product mixture was discharged from the reaction vessel after a retention time of about 1 second, at a temperature of about 244.degree. F., into a cooling vessel comprised of a cooling column where it ws cooled by a counter current air stream flowing at the rate of about 200 scfm per ton of reaction product mixture throughput per hour. The air and steam were vented as described above. The reaction product mixture was cooled to about 115.degree. F. at which temperature it was discharged into a receiving vessel. To the receiving vessel were added 0.6 parts by weight of anhydrous ammonia and 1.25 parts by weight of water, per hour. The 11-37-0 product formed had a pH of 6.4, a specific gravity of 1.435 and 58.5% of the P.sub.2 O.sub.5 was in poly form. The product was further cooled to about 108.degree. F. by indirect heat exchange with liquid ammonia and conducted from the receiving vessel to storage. Good results are also obtained when the procedure of Example XI is followed with the modification that the counter current cooling air stream flows at a rate of about 300 scfm per ton of reaction product mixture throughput per hour.
EXAMPLE XIIFollowing the procedure of Example VIII, to the reaction vessel are added, in parts by weight, 88 parts of superphosphoric acid having a P.sub.2 O.sub.5 content of 72.6 wt. %, 8.7 parts of anhydrous ammonia and 43 parts of water. The pressure drop across the reaction vessel is about 25 psi. The reaction product mixture is discharged from the reaction vessel after a retention time of about 10 seconds and a temperature of about 225.degree. F. into a cooling vessel equipped with cooling means. The product mixture is cooled in the cooling vessel to a temperature of about 103.degree. F. The product has a pH of 6.4, a specific gravity of 1.439 and 54%, of the P.sub.2 O.sub.5 is in poly form. Analyses of the product shows it contains 11% nitrogen and 37% P.sub.2 O.sub.5 corresponding to a grade of 11-37-0 fertilizer.
EXAMPLE XIIIThe procedure of Example VIII is followed with the modification that 70% of the total amount of ammonia required is added to the reaction vessel and the remainder is added through the sparger at the bottom of the receiving vessel. In like manner, 70% of the total amount of water required is added to the reaction vessel and the balance thereof added to the receiving vessel. A good 10-34-0 product is obtained.
The procedure of Example XIII is followed with the modification that the retention time in the reaction vessel is 30 seconds. A good product is obtained.
The procedure of this Example XIII is followed to produce 11-37-0 using the amounts given in Example XII. A good product is obtained.
EXAMPLE XIVThe procedure of Example VIII is followed with the modification that 99 wt. % of the total amount of ammonia required is added to the reaction vessel and the balance added through a sparger at the bottom of the receiving vessel; 99% of the total amount of the water required is added to the reaction vessel and the balance is added to the receiving vessel. A good 10-34-0 product is obtained.
EXAMPLE XVTo a reaction vessel of the kind described in Example VIII were added phosphoric acid having a P.sub.2 O.sub.5 content of 54 wt. % at the rate of 112 parts by weight per hour; anhydrous ammonia, 21 parts by weight per hour, and water, 80 parts by weight per hour. The pressure drop across the reaction vessel was about 40 psi. The reaction product mixture was discharged from the reaction vessel after a retention time of about 0.1 second, at a temperature of about 230.degree. F., into a cooling vessel comprised of a cooling column where it was cooled by a counter current air stream flowing at the rate of about 100 scfm per ton of reaction product mixture throughput per hour. The air and steam were vented as described above. The reaction product mixture was cooled to about 110.degree. F. at which temperature it was discharged into a receiving vessel. To the receiving vessel were added 2.5 parts by weight of anhydrous ammonia and 11 parts by weight of water per hour. The 10-34-0 product formed had a pH of 6.8, a specific gravity of 1.40 and 57.1% of the P.sub.2 O.sub.5 was in poly form. The product was further cooled to about 100.degree. F. and conducted from the receiving vessel to storage.
Good results are also obtained when the procedure of Example VIII is followed with the modification that the counter current cooling air stream flows at a rate of about 50 scfm per ton of reaction product mixture throughput per hour.
The procedure of Example VIII is followed with modifications in which the retention time is permitted to vary from 0.1 seconds to 8 minutes. A good 10-34-0 product is obtained at retention times within this range.
The procedure of Example VIII is followed with the modification that additional water is used to make as 8-24-0 product having a specific gravity of 1.28.
The procedures for Examples VIII through XIV are more fully set forth in the description relating to the process and apparatus earlier in this specification and as shown in the drawings. In each case the pH and the specific gravity are monitored and the amount of ammonia and water added to the acid is controlled to obtain the desired product.
The procedure of Example XV is followed with the modification that the phosphoric acid employed had a P.sub.2 O.sub.5 content of 40 wt. %. This acid is added at the rate of 150 parts by weight per hour. Anhydrous ammonia is added at the rate of 21 parts by weight per hour, and water is added at the rate of 40 parts by weight per hour. A product similar to that of Example VIII is obtained. A good product is obtained when phosphoric acid having a P.sub.2 O.sub.5 content of 53% is employed in the process of Example XV, and also when phosphoric acid having a P.sub.2 O.sub.5 content of 62% is employed and water is added at the rate of 100 parts by weight per hour.
Reaction temperatures below about 225.degree. F., as for example 150.degree. F., are employed when the method of this invention is carried out under pressures which are sufficiently reduced to bring about boiling of the reaction product mixture at the reaction temperature. The apparatus used for reduced pressure work is well known and commercially available and will not be described here.
Additional examples of runs made using the process of this invention are contained in the following Tables I, II, III IV, V(a) and V(b).
TABLE I
__________________________________________________________________________
RUN NUMBER 1 2 3 4 5 6 7
__________________________________________________________________________
COMPONENTS FED TO REACTION VESSEL:
Phosphoric Acid (P.A.)
(a) wt. % P.sub.2 O.sub.5 content
72.3 73.1 72.6 72.5 71.8 71.8 72.7
(b) percent of P.sub.2 O.sub.5 in Poly Form
56.1 60.7 56.5 59.0 59.2 57.5 59.6
(c) P.A. added (parts by wt./unit time)
4040 3090 3350 9890 8850 8480 8900
Ammonia added, (Parts by wt./unit time)
900 750 660 2340 2100 2100 1900
Water added, (Parts by wt./unit time)
4850 3500 4275 11000
11000
12500 9900
Pressure drop across Reaction Vessel psi.
28 28 25 45 40 42 45
Reaction Vessel Exit Temp .degree.F.
245 244 225 230 225 230 230
Retention time (in Reaction Vessel)
0.1 Sec.
0.1 Sec.
0.1 Sec.
0.1 Sec.
0.1 Sec.
0.1 Sec.
0.1 Sec.
Cooling Tower Exit Temp .degree.F.
110 115 108 105 110 98 95
Cooling Tower air, acfm/ton reaction pro-
duct mixture throughput per hour
390 410 550 230 175 510 340
COMPONENTS FED TO REACTION PRODUCT
MIXTURE RECEIVING VESSEL:
Ammonia added (parts by wt./unit time)
150 60 210 250 200 100 150
Water added (parts by wt./unit time)
175 125 160 1100 1100 1750 600
pH of End Product 6.45 6.40 6.40 6.8 7.1 6.4 5.
Specific gravity of End Product
1.440
1.435
1.439
1.400
1.402
1.404 1.470
Percent P.sub.2 O.sub.5 in poly form in end product
54.2 58.5 54.0 57.1 58.3 54.5 57.3
Temp. of product to storage, .degree.F.
105.degree.
108.degree.
103.degree.
100.degree.
74.degree.
92.degree.
98.degree.
Grades of N--P.sub.2 O.sub.5 --K.sub.2 O fertilizer produced
11-37-0
11-37-0
11-37-0
10-34-0
10-34-0
10-34-0
12-43-0
__________________________________________________________________________
TABLE II
__________________________________________________________________________
RUN NUMBER 1 2 3 4 5 6 7 8 9
__________________________________________________________________________
COMPONENTS FED TO REACTION VESSEL:
Phosphoric Acid (P.A.)
(a) wt. % P.sub.2 O.sub.5 content
80 69 86 70 70 80 71 78 78
(b) percent of P.sub.2 O.sub.5 in Poly Form
84 43 95 30 30 84 52 70 70
(c) P.A. added (parts by wt./unit time)
1290
1620
10,000
7100
4,810
11,500
6,692
10,300
10,300
Ammonia added, (Parts by wt./unit time)
350 350 3,500
1900
1,100
3,110
1,558
2,700
2,700
Water added, (Parts by wt./unit time)
800 650 17,350
5174
5,500
14,000
7,693
12,270
12,270
Pressure drop across Reaction Vessel psi.
1 2 100 45 10 80 20 60 60
Reaction Vessel Exit Temp .degree.F.
150.degree. F.
150.degree. F.
350.degree. F.
400.degree. F.
200.degree. F.
300.degree. F.
220.degree. F.
250.degree.
218.degree.
F.
Retention time (in Reaction Vessel)
8 min.
15 min.
0.1 sec
0.1 sec
0.3 sec
0.1 sec
0.1 sec
0.5
3 min.
Cooling Tower Exit Temp .degree.F.
80.degree. F.
80.degree. F.
150.degree. F.
150.degree. F.
120.degree. F.
120.degree. F.
100.degree. F.
100.degree.
100.degree.
F.
Cooling Tower air, scfm/ton reaction pro-
duct mixture throughout per hour
4000
3800
220 270 600 240 430 360 360
COMPONENTS FED TO REACTION PRODUCT
MIXTURE RECEIVING VESSEL:
Ammonia added (parts by wt./unit time)
30 30 300 300 100 200 135 200 200
Water added (parts by wt./unit time)
35 35 1,200
1000
30 625 200 300 300
pH of End Product 5.90
5.90
7.00
7.00
6.20
6.25
6.20
6.25 6.25
Specific gravity of End Product at 80.degree. F.
1.52
1.56
1.41
1.41
1.40
1.45
1.40
1.38 1.35
Percent P.sub.2 O.sub.5 in poly form in end product
75 41 70 50 25 75 50 65 65
Temp. of product to storage, .degree.F.
79 79 120 120 110 110 115 125 125
Grades of N--P.sub.2 O.sub.5 --K.sub.2 O fertilizer produced
12-43-0
12-43-0
12-33-0
12-33-0
10-34-0
11-37-0
10-34-0
11-37-0
11-37-0
__________________________________________________________________________
TABLE III
__________________________________________________________________________
ANALYSES OF POLYPHOSPHATE LIQUID FERTILIZER
REACTION PRODUCTS FROM NON HEATED
ORTHOSPHOSPHORIC ACID FEED
Components in Percent By Weight
Reaction % P.sub.2 O.sub.5
Vessel
% As Poly- % % % %
Material
Temp. .degree.F.
P.sub.2 O.sub.5
phosphate
%N Solids
Fe.sub.2 O.sub.3
Al.sub.2 O.sub.3
MgO
pH Sp. Gr.
N/P.sub.2 O.sub.5
__________________________________________________________________________
Feed Acid
-- 51.75
-- -- 2.18
1.04
2.01
0.39
-- -- --
Reaction
Product
500 27.80
32.80 7.31
6.98
0.67
1.06
0.22
-- -- --
Reaction
Product
460 32.94
30.94 10.63
2.77
-- -- -- 6.85
1.395
0.322
Reaction
Product
460 31.55
26.34 10.63
5.80
-- -- -- 7.10
1.373
0.337
Reaction
Product
455 48.23
35.72 13.98
5.22
-- -- -- 6.65
(Molten)
0.289
__________________________________________________________________________
TABLE IV
__________________________________________________________________________
ANALYSES OF POLYPHOSPHATE LIQUID FERTILIZER REACTION
PRODUCTS FROM PREHEATED ORTHOPHOSPHORIC ACID FEED
Components in Percent By Weight
%
Reaction
P.sub.2 O.sub.5
Pre-
Vessel As Poly-
Heat
Temp.
% Phos-
% % % % % %
Material
.degree.F.
.degree.F.
P.sub.2 O.sub.5
phate
N Solids
Fe.sub.2 O.sub.3
Al.sub.2 O.sub.3
MgO
SO.sub.4
pH Sp. Gr.
N/P.sub.2 O.sub.5
__________________________________________________________________________
Feed Acid
-- -- 52.55
-- -- 2.54
0.94
2.25
0.45
4.56
Reaction
Product 1
-- 450 31.61
20.12
8.70
2.03
-- -- -- -- 5.30
1.404
.275
Reaction
Product 2
-- 460 32.56
20.70
9.12
1.13
-- -- -- -- 5.40
1.406
.280
Reaction
Product 3
-- 480 31.66
23.28
9.25
0.91
-- -- -- -- 5.50
1.390
.292
Reaction
Product 4
250
490 32.04
37.55
9.75
0.91
-- -- -- 5.70
1.393
.304
Reaction
Product 5
280
490 30.67
43.36
10.25
0.15
-- -- -- -- 6.30
1.381
.334
Reaction
Product 6
-- 475 34.26
31.38
11.25
0.89
-- -- -- -- 6.45
1.442
.328
Reaction
Product 7
-- 480 31.68
36.02
10.54
0.27
-- -- -- -- 5.95
1.390
.332
Reaction
Product 8
-- 475 32.38
35.18
10.24
0.97
-- -- -- -- 6.20
1.410
.316
Reaction
Product 9
-- 475 31.41
33.14
10.52
0.57
-- -- -- -- 6.70
1.392
.335
Reaction
Product 10
310
495 28.98
37.85
9.25
0.18
-- -- -- -- 6.00
1.358
.319
Reaction
Product 11
300
480 29.70
39.70
8.95
0.25
-- -- -- -- 5.70
1.355
.301
__________________________________________________________________________
TABLE V-A
__________________________________________________________________________
ANALYSES OF POLYPHOSPHATE LIQUID FERTILIZER REACTION
PRODUCTS FROM PREHEATED ORTHOPHOSPHORIC ACID FEED
Components in Percent By Weight
%
Reaction
P.sub.2 O.sub.5
Pre-
Vessel Al Poly-
Heat
Temp.
% Phos-
% % % % % %
Material
.degree.F.
.degree.F.
P.sub.2 O.sub.5
phate
N Solids
Fe.sub.2 O.sub.3
Al.sub.2 O.sub.3
MgO
SO.sub.4
pH
Sp. Gr.
N/P.sub.2 O.sub.5
__________________________________________________________________________
Feed Acid
-- -- 54.16
-- -- 1.88
1.05
2.10
0.35
2.70
--
-- --
Reaction
Product 1
280
495 32.03
25.66
10.87
-- -- -- -- -- --
-- .339
Reaction
Product 2
295
495 36.95
37.08
10.78
-- -- -- -- -- --
-- .291
Reaction
Product 3
310
500 34.32
41.05
9.80
-- -- -- -- -- --
-- .286
Reaction
Product 4
310
500 35.39
43.43
10.72
-- -- -- -- -- --
-- .303
Reaction
Product 5
310
500 33.83
46.94
10.18
-- -- -- -- -- --
-- .301
Reaction
Product 6
310
500 33.35
44.62
9.83
-- -- -- -- -- --
-- .295
Reaction
Product 7
350
505 34.30
49.42
10.55
-- -- -- -- -- --
-- .308
Reaction
Product 8
350
510 34.26
47.49
9.81
-- -- -- -- -- --
-- .286
Reaction
Product 9
370
515 33.12
55.80
9.73
0.18
-- -- -- -- --
-- .294
Reaction
Product 10
375
525 33.85
59.79
10.04
0.18
-- -- -- -- --
-- .296
Reaction
Product 11
380
535 34.08
66.05
10.23
0.20
-- -- -- -- --
-- .301
Reaction
Product 12
400
575 52.65
68.24
10.17
0.13
-- -- -- -- --
-- .312
__________________________________________________________________________
TABLE V-B
__________________________________________________________________________
OPERATING CONDITIONS FOR PRODUCTION OF
POLYPHOSPHATE LIQUID FERTILIZER FROM
ORTHOPHOSPHORIC ACID
TEMPERATURES PRESSURES
RUN Reaction
Feed FLOWS, IN PART BY WEIGHT
Nos. corres-
Feed
Reaction
Vessel
Acid
Reaction Process
Product
pond to Nos.
Acid
Vessel
Discharge
Pump
Vessel
Acid Ammonia
Water Approx.
in Table V-A
.degree.F.
.degree.F.
.degree.F.
psig
psig Parts/Min.
Parts/Min.
Parts/Min.
Parts/Min.
__________________________________________________________________________
1 280
495 165 40 43 540 330 460 1100
2 295
495 165 40 32 540 300 460 1100
3 310
500 170 40 32 540 300 460 1100
4 310
500 165 40 32 540 300 460 1100
5 310
500 165 42 33 540 300 460 1100
6 310
500 165 42 33 540 300 460 1100
7 350
505 165 44 34 540 300 460 1100
8 350
510 185 40 35 540 300 460 1100
9 370
515 170 30 28 590 320 500 1200
10 375
525 185 32 29 590 320 500 1200
11 380
535 200 34 30 645 360 550 1300
12 400
575 205 38 33 645 370 550 1300
__________________________________________________________________________
In the above tables, the balance of the compositions of the feed acids and of the fertilizer products is made up substantially of water.
The in-line-mixing and reacting invention has been described hereinabove with illustrative examples and drawings of typical equipment that can be used in carrying out the process of this invention; however, such examples and illustrations are to be taken by way of example only and not by way of limitation. The invention is to be construed broadly within its spirit and scope as set forth in the following claims:
Claims
1. A continuous process for the manufacture of a liquid ammonium polyphosphate fertilizer, by a rapid ammoniation which minimizes loss of polyphosphates, from water, ammonia, and a phosphoric acid selected from the group consisting of orthophosphoric acid, polyphosphoric acid and mixtures thereof, said process comprising the steps:
- (a) forming, in a reaction zone in a reaction vessel, an entrained co-current stream reaction mass comprising water, ammonia and phosphoric acid, said water comprising water present in a phosphoric acid solution or added water;
- (b) permitting the ammonia to react exothermically with the phosphoric acid in said entrained stream reaction mass in said reaction zone to liberate heat and form a reaction product mixture comprising ammonium salts of the phosphoric acid and steam, said steam comprising both water converted to steam and water of constitution driven from at least two molecules of a material selected from the group consisting of phosphoric acid, polyphosphoric acid, ammonium phosphate, ammonium polyphosphate, and mixtures thereof, the pressure of said steam aiding in propelling the reaction mixture through and expelling it from said reaction zone;
- (c) quenching said reaction mixture with water to form a quenched reaction mixture;
- (d) separating steam from said quenched reaction mixture to produce a steam-separated reaction product; and
- (e) further cooling said steam-separated reaction product by heat exchange with air to a temperature in the range of about 80.degree. F. to about 150.degree. F. to form a cooled product comprising an aqueous solution of ammoniated species of both ortho and polyphosphoric acids.
2. The process of claim 1 wherein said quenching is effected prior to discharge of said reaction mixture from said reaction vessel.
3. The process of claim 1 wherein said quenching is effected after discharge of said reaction mixture from said reaction vessel.
4. The process of claim 1 wherein said reaction mixture is permitted to reside in said reaction zone for a period of from about 0.1 seconds to about 15 minutes.
5. The process of claim 1 wherein said reaction mixture is permitted to reside in said reaction zone for a period of from about 1 second to about 3 minutes.
6. The process of claim 1 wherein the temperature in said reaction zone is maintained within the range of from about 400.degree. F. to about 700.degree. F.
7. The process of claim 6 wherein the components are fed into said reaction zone at a pressure sufficient to maintain a pressure in said reaction zone of from about 0.1 to about 100 psi.
8. The process of claim 1 wherein the temperature in said reaction zone is maintained within the range of from about 450.degree. F. to about 650.degree. F.
9. The process of claim 8 comprising,
- employing in said reaction mixture only a part of the ammonia required to form an end product having a predetermined pH in the range of from about 3.5 to about 8.5, and
- adding ammonia to, and allowing it to react with said cooled product to produce an end product having said predetermined pH.
10. The process of claim 9 wherein:
- the amount of ammonia employed in said reaction mixture is from about 70 weight percent to about 99 weight percent of the required ammonia to produce an end product having a predetermined pH within the range of from a out 3.5 to about 8.5, and
- the balance of said required ammonia is added to said cooled product.
11. The process of claim 1 comprising,
- employing in said quenched reaction mixture only a part of the water required to form an end product having a predetermined specific gravity, and
- adding water to said cooled product in an amount sufficient to obtain said end product having said predetermined specific gravity.
12. The process of claim 11 wherein the specific gravity of said end product is from about 1.3 to about 1.5.
13. The process of claim 1 wherein said phosphoric acid is admitted to said reaction zone at a temperature of from about 70.degree. F. to about 575.degree. F.
14. A continuous process for the manufacture of a liquid ammonium polyphosphate fertilizer, by a rapid ammoniation which minimizes loss of polyphosphates, from water, ammonia, and a phosphoric acid, polyphosphoric acid and mixtures thereof, said process comprising the steps:
- (a) forming, in a reaction zone in a reaction vessel, an entrained co-current stream reaction mass comprising water, ammonia and phosphoric acid, said phosphoric acid being at a temperature of from about 70.degree. F. to about 575.degree. F. when admitted to said reaction zone, said water comprising water present in a phosphoric acid solution or added water, and said ammonia being from about 70 weight percent to about 99 weight percent of the required ammonia to produce an end product having a predetermined pH within the range of from about 3.5 to about 8.5;
- (b) permitting the ammonia to react exothermically with the phosphoric acid in said entrained stream reaction mass in said reaction zone at a temperature in the range of about 400.degree. F. to about 700.degree. F. to liberate heat and form a reaction product mixture comprising ammonium salts of the phosphoric acid and steam, said steam comprising both water converted to steam and water of constitution driven from at least two molecules of a material selected from the group consisting of phosphoric acid, polyphosphoric acid, ammonium, phosphate, ammonium polyphosphate, and mixtures thereof, the pressure of said steam aiding in propelling the reaction mixture through and expelling it from said reaction zone;
- (c) quenching said reaction mixture with water for form a quenched reaction mixture, said water being less than the required water to form an end product having a predetermined specific gravity;
- (d) separating steam from said quenched reaction mixture to produce a steam-separated reaction product;
- (e) further cooling said steam-separated reaction product by heat exchange with air, to a temperature in the range of about 80.degree. F. to about 150.degree. F., to form a cooled product comprising an aqueous solution of ammoniated species of both ortho and polyphosphoric acids; and
- (f) adding the balance of said required ammonia and required water to said cooled product to obtain said end product having said predetermined pH in the range of from about 3.5 to about 8.5 and said predetermined specific gravity.
15. A process for the manufacture of an ammonium polyphosphate fertilizer from water, ammonia, and a phosphoric acid selected from the group consisting of orthophosphoric acid, polyphosphoric acid and mixtures thereof, comprising the steps:
- (a) forming an entrained co-current stream reaction mass comprising water, ammonia and phosphoric acid, said water comprising water present in a phosphoric acid solution or added water;
- (b) permitting the ammonia to react exothermically in a reaction zone with the phosphoric acid in said entrained co-current stream reaction mass to liberate heat and form a reaction product mixture comprising ammonium salts of the phosphoric acid and steam, said steam comprising both water converted to steam and water of constitution driven from at least two molecules of a material selected from the group consisting of phosphoric acid, polyphosphoric acid, ammonium phosphate, ammonium polyphosphate, and mixtures thereof: and,
- (c) quenching said reaction product mixture with water in order to form a final product mixture comprising an aqueous solution of ammoniated species of both ortho and polyphosphoric acids.
16. The process of claim 15 wherein said reaction zone is in a reaction vessel which further contains a quenching zone after said reaction zone and an air cooling zone after said quenching zone and wherein said final product mixture is further cooled by means of air in said air cooling zone prior to discharge from said reactor.
17. The process of claim 16 wherein the temperature in said reaction zone is maintained within the range of from about 450.degree. F. to about 525.degree. F.
18. In a continuous process for manufacture of an ammonium polyphosphate fertilizer solution, the steps comprising:
- (a) introducing ammonia, water and superphosphoric acid analyzing at least about 69% P.sub.2 O.sub.5 into a reaction zone in a reaction vessel;
- (b) permitting the ammonia to react exothermically within said reaction zone with said superphosphoric acid to liberate heat and form an entrained co-current stream reaction mass comprising steam and ammonium salts of superphosphoric acid;
- (c) allowing said steam to rapidly move said reaction mass through said reaction zone and cause a liquid ammonium superphosphoric acid solution to be discharged from said reaction vessel, said fertilizer containing at least a majority of the polyphosphates contained in said superphosphoric acid.
19. The process of claim 18 wherein the numerical value of said polyphosphate analysis of said fertilizer is no less than at least about 73.6% of the polyphosphate analysis of said superphosphoric acid.
20. A process for the manufacture of an ammonium polyphosphate fertilizer from water, ammonia, and a phosphoric acid selected from the group consisting of orthophosphoric acid, polyphosphoric acid and mixtures thereof, comprising:
- (a) continuously reacting ammonia and said phosphoric acid in the presence of water in an entrained cocurrent stream with the liberation of heat to remove water of constitution, and to form steam and a reaction product comprising an ammonium polyphosphate, said steam comprising vaporized water and vaporized water of constitution from at least one member of the group consisting of said phosphoric acid and said reaction product; and,
- (b) quenching said reaction product with water in order to form an aqueous product mixture comprising ammonium polyphosphate.
| 3323863 | June 1967 | Seymour |
| 3419378 | December 1968 | Kearns |
| 3562778 | February 1971 | Siegel et al. |
| 3677734 | July 1972 | Carroll et al. |
| 1001984 | August 1965 | GBX |
- Condensed Chem. Dict., Hawley, p. 688, Phosphoric Acid, 1971. Phosphroic Acid, Phosphates & Phosphate Fertilizers, Waggaman, 1962, pp. 174-175.
Type: Grant
Filed: Jan 7, 1980
Date of Patent: Jun 15, 1982
Assignee: Leather's Chemical Company, Limited (Yeadon, Leeds)
Inventors: John D. Ellis (Upland, CA), George Crichton (Guadalajara, NM), Millard C. Godwin (Lakeland, FL), George C. Morris (Lakeland, FL)
Primary Examiner: S. Leon Bashore
Assistant Examiner: Ferris H. Lander
Attorneys: Barry A. Bisson, William N. Patrick
Application Number: 6/110,152
International Classification: C05B 700;
